modelling & experimental validation of biomass-steam ... · 1−ε mf) l mf a c ( ) ( ) 3...
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![Page 1: Modelling & experimental validation of biomass-steam ... · 1−ε mf) L mf A c ( ) ( ) 3 '2 2 ' 2 3 1 1.75 150 p f mf mf mf mf p mf f mf mf mf mf d u L P μ ε ρ−ε −Δ = +](https://reader031.vdocuments.net/reader031/viewer/2022011910/5f8354706760c56b350fd360/html5/thumbnails/1.jpg)
Modelling & experimental validation of biomass-steam gasification in bubbling fluidized bed reactor
Prasanth Gopalakrishnan
Supervisor: Professor Shusheng PangCo-supervisor: Dr Chris Williamson
Department of Chemical and Process Engineering
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Objective:
To develop a mathematical model to simulate the gas composition of biomass gasification in the bubbling fluidised gasifier.
Unsteady state non isothermal model based on reaction kinetics of produced combustible gases.
Investigation of the effects of operating parameters such as temperature and steam to biomass ratio on the gas compositions.
Validate the model with experimental data
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Fluidised Bed- Gasification Technology with Steam as Gasification Agent
Biomass
Char &
Sand
Combustible Gases
CO2 ,CO, H2, H2O, CH4
BFB
Gasifier
CFB
Combustor
Hot Sand
SteamAir
Flue gas
43.88O
0.03N
7.31H
48.28C
Wt % dry basisUltimate AnalysisBiomass - Pinus radiata
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Gasifier at UoC
• Leads a programme on ‘Wood IGCC’ for wood industry.
• Has built a 100 kWthlaboratory-scale Fast Internal Circulating Fluidised Bed (FICFB) Gasifier for tests and evaluation of radiata pine residues.
• Developing producer gas cleaning technologies.
• Biofuels projects (Pyrolysis, Fischer-Tropsch process).
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Biomass gasification• There are two stages of physical and chemical changes in the
biomass gasification:– Decomposition of the biomass under high temperature. This is a
similar process to biomass fast pyrolysis. – Secondary reactions involving the evolved volatiles.– Char reaction with gasification agent.
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Instantaneous Overall Pyrolysis Reactions
CharNTarN
HCNCHNHN
OHNCONCON
H
OHNOCHN
chartar
HCCHH
OHCOCOmoistwood
+
+++
+++⎯⎯⎯⎯ →⎯+
Temphighvery
at eat
4242
222 66.044.1
4242
22
For reaction above (fast pyrolysis in fluidized bed) a product distribution,instead of a “typical” kinetic equation, was defined by Gonza´lez-Saiz, in his PhD Thesis “Advances in biomass gasification in fluidized bed”, with the same type of biomass as the one considered in our research (small pine wood chips) and in a fluidized bed working under similar experimental conditions(Sadaka et al., 2002)
yi= Function (Temperature) i corresponds to volatile gases & tar and char
can be used as initial condition
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Secondary Reactions Involved in the evolved volatiles and Gasification of char reactions
22
1
on Gasificati Steam HCOOHCK
+⇔+
222
2
Reaction shift -gasWater HCOOHCOK
+⇔+
42
3
2 Reaction n Methanatio CHHCK
⇔+
[J/mol]
oGΔ
[J/mol]
oHΔ
-3262170.47~ 820
-63988-119.37~1098
124978-164.21~948
Equilibrium temperature[K]
Reactions
222 225
HCOOHCK
+⇔+ 6306542.75~903
COCOCK
2 Reaction Bouduard4
2 ⇔+
224 3 Reaction Reforming
Methane Steam6
HCOOHCHK
+⇔+ 157224-111.52~ 893
187667251.87~973
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Bubble Region
Emulsion Region
Ub Ue
Ab Ae
Fbe
Biomass Feed
Hb
Producer Gas
Tbed
Inlet Steam at velocity of Uo
D1D2
Fast Pyrolysis Zone
Gasification Zone
Fig.1 Two phase model for fluidised bed gasifier.
Hydrodynamic model of Fluidization
•Mixing & distribution of solids & fluid – “Emulsion Region”
•Formation of motion of bubbles through the bed – “Bubble Region”
•Interphase mass transfer of particles and gases between the regions Fbe
•Emulsion phase – plug flow and all reactions occurs in this region
•Bubble phase – no solids, only water gas reaction and methane reforming reaction occurs.
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Mass Balance
Accumulation
of species (i) = + -
( ) ibieibbeib
ibib
bib RCCF
xCD
xCU
tC
+−−∂∂
+∂∂
−=∂∂
2
2
Bubble phase Mass balance
Accumulation of species (i)
{rate of i in– rate of i out } convection
rate of i out by exchangewith the emulsion phase
Chemical Reaction term
rate of i in –rate of i out
convection
rate of production
of i by chemical
reaction
rate of i out by exchange withthe emulsion phase
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Emulsion phase Mass balance
( ) ieieibemf
bbeieie
ib
mf
eie RCCAAF
xC
Dx
CUt
C+−+
∂∂
+∂∂
−=∂∂
εε 2
2
Accumulation
of species (i){rate of i in– rate of i out } convection
rate of i into the emulsion phase by exchange withbubble phase
Chemical Reaction term involved in emulsion phase
+ rate of production of species by devolatilization
of feed
Conc. of ithspecies[Kgmol/m3]
Emulsion phase gas velocity [m/s]
Diffusion co-efficient of Component i [m2/s]
Gas Exchange Coefficient b/n Bubble & emulsion phase [1/s]
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Energy Balance
Rate of heat accumulation in the emulsion phase
=
heat in by gas flow in the emulsion phase
-
heat out by gas flow in the emulsion phase
+
Net heat exchange b/nthe bubble & Emulsion phase
+/-
heat generated by reactions in the emulsion phase
+
Heat input by bed material in
-
Heat removed by bed material char out
* Similarly for the bubble phase except all the terms applies except the last two terms
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( ) ( ) ribbbebebibibbbpbib HRTTHHCU
xtTCC
Δ+−+Δ∂∂
=∂
∂∑ δδ
Bubble phase Energy balance
Rate of heat accumulation in the bubble phase
heat in by gas flow in the emulsion phase
-
heat out by gas flow in the emulsion phase
Net heat exchange b/nthe bubble & Emulsion phase
heat generated by reactions in the emulsion phase
Sensible heat [kJ/kmol]
Heat interchange coefficient b/nbubble & emulsion phase [kW/m3K]
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( ) ( ) ( )
( )x
TCmHR
TTHHCUxt
TCC
psandsandrie
ebbeieieeepeie
∂
∂+Δ−+
−−+Δ∂∂
=∂
∂
•
∑
δ
δ
1
1
Heat input by bed material in
-
Heat removed by bed material char out
Emulsion phase Energy balance
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Boundary Conditions
x=0
x=H
01
iib
bib C
xC
UDC =
∂∂
− 02
iie
eie C
xC
UDC =
∂∂
−
;
0=∂∂
xC ib 0=
∂∂
xCie
;
0=∂∂
xTb 0=
∂∂
xTe
;
ineb TTT ==
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Hydrodynamics of Fluidized Bed
Gravitational force :
Pressure drop given by
Ergun’s Correlation of fixed bed
( ) ( )( ) cmfmffpappBcmf ALgVggWAP ερρρ −−===Δ− 1,
( ) ( ) ( )2'3
2
'
2
3
1150
175.1
p
mfmff
mf
mf
p
mffmf
mf
mfmf d
Lud
LuP
μεερ
εε −
+−
=Δ−
•At minimum Fluidization,bed starts lifting.
•At this point the frictional upward lift force just exceeds the gravitationalforce.
( ) ( )0
75.175.11150 '3
'2 =
−−
−+
f
pmffpmf
pf
fmfmf
dgu
du
ρερρ
ρμε
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Hydrodynamics of Fluidized Bed (Continues…)Some variables involved in the model are closely interrelated through
hydrodynamics derived from (Mori and Wen, 1975) and (Davidson et al., 1985)
Bubble diameter: Maximum Bubble diameter: Initial bubble diameter:
Bubble velocity:Volume fraction of bubble:Emulsion velocity:
Gas exchange co efficient b/n bubble & emulsion phase [1/s]
( ) ( )DxDDDD bbMbMb /3.0exp0 −−−=
( )[ ] 4.0064.1 mfbM UUAD −=
( )[ ] 4.000 /871.0 NUUAD mfb −=
( ) 5.00 711.0 bmfb gDUUU +−=
( ) bmf UUUDEL /0 −=
( )DELUUe mf −= 1
bbe DF 11.0=
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Operating Conditions
• Arrhenius reaction type is used• Temperature : 760 Deg C• Feed rate : 20 kg/hr• Steam/Biomass: 0.3• Initial volatiles after instant fast pyrolysis
CH2,0= 0.0051 kmol/m3 (29.81 mol %)CCO,0 = 0.0067 kmol/m3 (39.2 mol %)CCO2,0= 0.0023 kmol/m3 (13.62 mol%)CCH4,0= 0.0021 kmol/m3 (12.2 mol %)
• Initial concentration of steam ,CH2O,0= 0.0015 kmol/m3
• Mass of Tar formed during Initial pyrolysis =1.41 kg• Mass of char formed during Initial pyrolysis =2.99 kg
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Experiment Results from published literature data
(Lv, Chang et al. 2004)
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Height X
Height X
Simulation results
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01
2
0
0.5
10.2
0.3
0.4
Height xTime t[hr]
y H2
01
2
0
0.5
10.2
0.3
0.4
0.5
Height xTime t[hr]
y CO
01
2
0
0.5
10
0.2
0.4
Height xTime t[hr]
y CO
2
01
2
0
0.5
10.05
0.1
0.15
0.2
Height xTime t[hr]
y CH
4
Simulation results
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(Gil et al., 1999)
Experiment Results from published literature data
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Steady State Gasifier Test showing the Transition Process from Heat-up to Gasification at the Start.
0
10
20
30
40
50
60
70
80
90
10015
.24
15.4
0
16.0
0
16.2
9
16.5
7
17.3
3
17.5
9
18.2
1
18.3
4
19.0
2
Sampling Time
Gas
Com
posi
tion
(vol
%)
0.0
2.0
4.0
6.0
8.0
10.0
12.0
14.0
16.0
Low
er H
eatin
g Va
lue
(MJ/
Nm
^3)
H2 % N2 % CO %CH4 % Ethene % Ethane %CO2 % He Lower Heating Value (MJ
.
Gasifier run on 03 March 08. Bed material: Sand (12.5kg)
Wood feed rate: 20 kg/hr ; Steam : 6 kg/hr ; S/B=0.3; Bed Temperature: 750 Deg C
Experimental results from the dual fluidized bed gasifier,UoC
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Producer Gas Composition Changes with Different Fluidizing Gases to the Chute & Siphon
0
10
20
30
40
50
60
70
80
90
100
14 15 16 17 18 19 20 21 22
DryWood pellets feed rate (Kgdry/h)
Gas
Com
posi
tion
(vol
%)
0
2
4
6
8
10
12
14
16
Low
er H
eatin
g Va
lue
(MJ/
Nm
3 )
H2 % N2 % CO % CH4 % Ethene % Ethane % CO2 % He % Lower CV (MJ/Nm3)
Gasifier run: Bed material: Sand (12.5kg); Wood feed rate: 14.2 - 21.25 kg/hr; Steam : 6 kg/hr ; S/B=0.28-0.45; avg bed temperature: 800 Deg C
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Gas Composition on Dry Basis
0
10
20
30
40
50
60
0 1 2 3 4 5 6
Biomass-Steam Ratio
Mol
e Fr
actio
n
H2COCO2CH4
Gas Composition on Dry Basis
05
10152025303540
0.2 0.4 0.6 0.8 1
Biomass-Steam Ratio
Mol
e Fr
actio
n
H2COCO2CH4
Effect of Steam to Biomass Ratio when pine is gratified at 800 Deg C
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Gas Composition on Wet Basis
0
5
10
15
20
25
30
35
40
45
50
0 1 2 3 4 5 6 7
Biomass-Steam Ratio
Mol
e Fr
actio
n H2COCO2CH4H2O
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(Franco et al., 2003)
Experiment Results from published literature data
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Effects of Temperature and Steam to Biomass Ratio
• Effects of Increase in TemperatureI. H2 and CO increased
II. CO2 and CH4 decreased
• Effects of Increase in Steam to Biomass ratio.I. CO2 increased
II. CO and H2 decreased
III. CH4 insignificant change ( remains unchanged)
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Extension of the work
•Reaction kinetics of tar and higher hydrocarbon can be included.
•Parameters such as D1 and D2 are the axial dispersion co-efficient for the bubble to emulsion and Emulsion to bubble phase. The valuesare taken such as D1 constitutes to plug flow and D2 to mixed flow.
• It is recommended to use the diffusion co-efficient of the individual gas components. Finding the appropriate values for the dispersion co-efficient for individual gas components involved in the reactions between the phases, would improve the results.
• Both particle and gas phase void fractions are assumed to be constants. Hence continuity equation along with the momentum equation canbe incorporated to the non isothermal reaction kinetics model to evaluatethe changes in the void fraction along the length of the gasifier.
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References
DAVIDSON, J. F., CLIFT, R. & HARRISON, D. (1985) Fluidization, London Orlando: Academic Press.
FRANCO, C., PINTO, F., GULYURTLU, I. & CABRITA, I. (2003) The study of reactions influencing the biomass steam gasification process.Fuel, 82, 835-842.
GIL, J., CORELLA, J., AZNAR, M. P. & CABALLERO, M. A. (1999) Biomass gasification in atmospheric and bubbling fluidized bed: Effect of the type of gasifyingagent on the product distribution. Biomass and Bioenergy, 17, 389-403.
Lv, P. M., J. Chang, et al. (2004). "A kinetic study on biomass fast catalytic pyrolysis." Energy & Fuels 18(6): 1865-1869.
MORI, S. & WEN, C. Y. (1975) Estimation of bubble diameter in gaseous fluidized beds. AIChE Journal, 21, 109-115.
SADAKA, S. S., GHALY, A. E. & SABBAH, M. A. (2002) Two phase biomass air-steam gasification model for fluidized bed reactors: Part II--model sensitivity. Biomass and Bioenergy, 22, 463-477.
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